EP0564329A1 - Gruppe-VIII Metal und Gruppe-IIIA Metal an einem Träger enthaltender Katalysator - Google Patents

Gruppe-VIII Metal und Gruppe-IIIA Metal an einem Träger enthaltender Katalysator Download PDF

Info

Publication number
EP0564329A1
EP0564329A1 EP93400774A EP93400774A EP0564329A1 EP 0564329 A1 EP0564329 A1 EP 0564329A1 EP 93400774 A EP93400774 A EP 93400774A EP 93400774 A EP93400774 A EP 93400774A EP 0564329 A1 EP0564329 A1 EP 0564329A1
Authority
EP
European Patent Office
Prior art keywords
metal
catalyst
group
weight
support
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP93400774A
Other languages
English (en)
French (fr)
Other versions
EP0564329B1 (de
Inventor
Patrick Sarrazin
Jean-Paul Boitiaux
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
IFP Energies Nouvelles IFPEN
Original Assignee
IFP Energies Nouvelles IFPEN
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by IFP Energies Nouvelles IFPEN filed Critical IFP Energies Nouvelles IFPEN
Publication of EP0564329A1 publication Critical patent/EP0564329A1/de
Application granted granted Critical
Publication of EP0564329B1 publication Critical patent/EP0564329B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
    • C10G45/34—Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used
    • C10G45/40—Selective hydrogenation of the diolefin or acetylene compounds characterised by the catalyst used containing platinum group metals or compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/08—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of gallium, indium or thallium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/56—Platinum group metals
    • B01J23/62—Platinum group metals with gallium, indium, thallium, germanium, tin or lead
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/825—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with gallium, indium or thallium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B01J37/0205—Impregnation in several steps
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
    • C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation

Definitions

  • the present invention relates to a catalyst containing a support, at least one metal of GVIII and at least one metal of GIIIA chosen from gallium and indium, in which the support is changed with the metal (s) of GIIIA then with the metal (s) of GVIII.
  • regenerable catalysts are prepared, by incorporation of at least one said additional catalytically inactive metal into the support, calcination, introduction of the GVIII metal and then of the additional catalytically active metal (for example indium ).
  • the metal of GVIII must be introduced before indium because otherwise "the advantageous influence of the additional metal on the behavior of the catalyst does not appear".
  • Such catalysts are applied to dehydrocyclization and reforming.
  • the hydrogenation reactions are generally carried out in a range of temperatures between 20 and 200 ° C, under a pressure between 10 and 100 bar (1 and 10 Megapascal) and with an hourly space velocity between 1 and 40 m3 / m3 catalyst / h.
  • the catalysts generally used consist of one or more metals deposited on an oxide support.
  • the preferred base metals are commonly those of group VIII and more particularly nickel, palladium and platinum.
  • the supports are, for their part, often chosen from alumina, silica, silica-aluminas, aluminates or even coal.
  • Said catalyst contains (a) at least one metal from group VIII chosen from nickel, palladium, platinum, rhodium and ruthenium (palladium, platinum and nickel being the preferred metals) and the percentage by weight of which is chosen between 0.1 and 10% and preferably between 0.2 and 5% and (b) at least one additional metallic element chosen from group III.A consisting of gallium and indium whose weight percentage is chosen between 0 , 01 and 10% and preferably between 0.1 and 5% and the molar ratio of group III metal element to group VIII metal is advantageously between 0.2 and 5 and preferably between 0.3 and 2 (c) a support, chosen from the group consisting of a silica, an alumina, a silica-alumina, an aluminate and a carbon.
  • group VIII chosen from nickel, palladium, platinum, rhodium and ruthenium (palladium, platinum and nickel being the preferred metals) and the percentage by weight of which is chosen between 0.1 and 10% and preferably between 0.2 and
  • the aluminates of the elements of groups I.A, II.A or II.B of the periodic table can be used such as, for example, the aluminates of Ca, Mg, Ba, Zn, Na, K, Cd and mixed aluminates
  • the catalyst can be prepared by different procedures.
  • a preferred procedure is the impregnation of the support, but the invention is not limited to a specific procedure.
  • the impregnation consists, for example, in bringing the preformed support into contact with an aqueous or organic solution of a compound of the metal or metals chosen from group III.A (gallium and indium) the volume of solution being in excess relative to the retention volume of the support or preferably equal to this volume.
  • the impregnated support is filtered, washed with distilled water, dried and calcined in air usually between 110 ° C and 600 ° C and preferably between 110 ° C and 500 ° C.
  • the catalyst Before depositing the metal or metals of group VIII, the catalyst can advantageously be reduced under hydrogen, it is usually carried out between 50 ° C and 600 ° C and preferably between 90 ° C and 500 ° C or using a organic reducing agent in solution. This operation further increases the activity of the catalyst.
  • the product obtained is then impregnated with an organic solution (hydrocarbon for example) or aqueous of a group VIII metal depending on the nature of the precursor used; in a particularly advantageous manner, a solution of palladium nitrate or nickel in water is used.
  • an organic solution hydrocarbon for example
  • aqueous of a group VIII metal depending on the nature of the precursor used; in a particularly advantageous manner, a solution of palladium nitrate or nickel in water is used.
  • the support thus impregnated is filtered, optionally washed with distilled water, then dried and calcined in air, usually between approximately 110 ° C. and approximately 600 ° C., and preferably between approximately 110 ° C. and approximately 500 ° C., then reduced under hydrogen at a temperature usually between about 50 ° C and about 600 ° C and preferably between about 80 ° C and about 500 ° C.
  • the elements of GVIII and GIII are then in the form of oxide and / or metal deposited on the support.
  • Another method is to knead the wet support powder with the catalyst precursors and then shape and dry.
  • metal precursors which can be used in the preparation of the catalyst are the following:
  • group VIII metal it is possible to use compounds such as chlorides, nitrates, halogen-amino compounds, amino compounds, salts of organic acids soluble in the impregnating solvent.
  • organometallic compounds of a group VIII metal in solution in an organic solvent, for example a hydrocarbon.
  • hydrocarbons mention may be made of saturated paraffinic hydrocarbons, the hydrocarbon chain of which contains from 6 to 12 carbon atoms per molecule, the naphthenic hydrocarbons which contain from 6 to 12 carbon atoms per molecule, or the aromatic hydrocarbons containing from 6 to 12 carbon atoms per molecule.
  • organometallic metal compounds of group VIII of: carbonyl, halocarbonyl compounds and acetylacetonates, without this list being limiting.
  • the element chosen from the group consisting of gallium and indium can preferably be introduced in the form of at least one inorganic compound chosen from the group formed by chlorides, nitrates, halo-amino compounds, compounds amino acids and salts of organic acids soluble in impregnating solvents.
  • metal III.A is advantageously carried out using an aqueous solution of the inorganic compound of said metal III.A.
  • the element chosen from the group consisting of gallium and indium can also be introduced via organometallic compounds in solution in an organic solvent, for example a hydrocarbon.
  • a hydrocarbon for example, hydrocarbons, mention may be made of saturated paraffinic hydrocarbons, the hydrocarbon chain of which contains from 6 to 12 carbon atoms per molecule, the naphthenic hydrocarbons which contain from 6 to 12 carbon atoms per molecule, or the aromatic hydrocarbons containing from 6 to 12 carbon atoms per molecule.
  • organometallic metal compounds from the group consisting of gallium and indium mention may be made of: alkyls, alkoxides, acetates and acetylacetonates without this list being limiting.
  • the support can be varied in nature, as already mentioned above.
  • a particularly suitable support has specific characteristics such as a specific area, determined by the BET method, of between 10 and 500 m2 per gram and preferably between 50 and 500 m2 per gram and a total pore volume of 0.2 to 1.3 cm3 per gram of support.
  • the catalyst advantageously undergoes an activation treatment under hydrogen at high temperature, for example 50-600 ° C., in order to obtain an active metallic phase.
  • the procedure for this treatment under hydrogen consists, for example, of a slow rise in temperature under a stream of hydrogen up to the maximum reduction temperature, for example between 50 ° C. and 600 ° C. and preferably between 80 ° C. and 500 ° C, followed by maintaining for example 1 to 6 hours at this temperature.
  • the hydrogen used is free of carbon monoxide.
  • the catalyst used consists of palladium at a content of 0.3% by weight deposited on a transition alumina with a specific surface area equal to 70 m2 / g. It is prepared by dry impregnation of a tetragonal gamma alumina with a pore volume equal to 0.6 cm3 / g using a solution of palladium nitrate. After impregnation, the sample is dried at a temperature of 120 ° C for 2 hours, then calcined under air flow at a temperature of 450 ° C for 2 hours. Before testing, the catalyst is reduced under hydrogen flow at a temperature of 150 ° C for 2 hours.
  • Example 2 the same reaction is carried out under the same conditions as in Example 1, but this time successively different catalysts containing 0.3% by weight of palladium and a variable gallium content are used.
  • the support used is identical to that of the monometallic catalyst A of Example 1. Different batches of this support are impregnated to dryness with solutions of gallium nitrate of variable concentrations. After impregnation, the samples are dried at a temperature of 120 ° C for 2 hours, then calcined under air flow at a temperature of 450 ° C for 2 hours. Palladium is then deposited using the same method as that described in Example 1 for catalyst A. Before testing, the catalysts are reduced under hydrogen flow at a temperature of 150 ° C for 2 hours.
  • the following table shows the composition of the product after 8 minutes of reaction for each of the catalysts identified by their gallium content as well as for the monometallic catalyst A of Example 1.
  • Ga content (% by weight) Butadiene (% by weight) Butenes (% by weight) Butane (% by weight) 0 9 90.7 0.3 0.07 6.57 93.16 0.27 0.21 5.55 94.2 0.25 0.42 7.5 92.22 0.28 0.82 8 91.7 0.3 1.19 10.3 89.4 0.3
  • the samples having a gallium content of between 0.07 and 0.82% by weight have a higher activity than that of the monometallic catalyst since after the same reaction time (8 minutes) the butadiene content of the product is lower .
  • these catalysts, which are more active than monometallic are also more selective with regard to the consecutive hydrogenation of butenes. In fact, although the conversion of butadiene is greater, it can be seen that the butene content is greater and that the formation of butane is reduced.
  • Example 2 the same reaction is carried out under the same conditions as in Example 1.
  • catalyst B is used containing 0.3% by weight of palladium and 0.24% by weight of gallium deposited on the same support as in Example 1 following the same preparation method as in Example 2.
  • a catalyst C having the same composition but which differs from catalyst B is also used in that the gallium precursor on alumina used during preparation a was reduced under hydrogen at a temperature of 450 ° C for 2 hours before the deposition of palladium.
  • the composition of the products obtained after 8 minutes of reaction is presented in the following table: Catalyst Butadiene (% by weight) Butenes (% by weight) Butane (% by weight) B 5.6 94.14 0.26 VS 4.2 95.53 0.27
  • catalyst C is more active than catalyst B with respect to the hydrogenation of butadiene.
  • a gain in selectivity is also observed since with a higher conversion to butadiene, the butene content is higher for catalyst C.
  • the hydrogen used is free of carbon monoxide.
  • the catalyst used is catalyst A of Example 1.
  • Example 2 the same reaction is carried out under the same conditions as in Example 1, but this time successively different catalysts containing 0.3% by weight of palladium and a variable gallium content are used.
  • the support used is identical to that of the monometallic catalyst A of example 1. Different batches of this support are dry impregnated with palladium nitrate using the same method as that described in example 1 for catalyst A. then deposits the gallium by impregnating solutions of gallium nitrate of variable concentrations. After impregnation, the samples are dried at a temperature of 120 ° C for 2 hours, then calcined under air flow at a temperature of 450 ° C for 2 hours. Before testing, the catalysts are reduced under a flow of hydrogen at a temperature of 150 ° C. for 2 hours.
  • the following table shows the composition of the product after 8 minutes of reaction for each of the catalysts identified by their gallium content as well as for the monometallic catalyst A of Example 1.
  • the samples having a gallium content of between 0.08 and 0.80% by weight have a higher activity than that of the monometallic catalyst of Example 1 since after the same reaction time (8 minutes) the content of butadiene of the product is lower.
  • these catalysts, which are more active than monometallic are also more selective with regard to the consecutive hydrogenation of butenes. Indeed, although the conversion of butadiene is greater, it is seen that the butene content is higher and that the formation of butane is reduced.
EP93400774A 1992-04-02 1993-03-24 Gruppe-VIII Metal und Gruppe-IIIA Metal an einem Träger enthaltender Katalysator Expired - Lifetime EP0564329B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR929204151A FR2689419B1 (fr) 1992-04-02 1992-04-02 Catalyseur contenant un métal du groupe VIII et un métal de groupe III a déposés sur un support, applicable à l'hydrogénation sélective des hydrocarbures.
FR9204151 1992-04-02

Publications (2)

Publication Number Publication Date
EP0564329A1 true EP0564329A1 (de) 1993-10-06
EP0564329B1 EP0564329B1 (de) 1997-12-03

Family

ID=9428513

Family Applications (1)

Application Number Title Priority Date Filing Date
EP93400774A Expired - Lifetime EP0564329B1 (de) 1992-04-02 1993-03-24 Gruppe-VIII Metal und Gruppe-IIIA Metal an einem Träger enthaltender Katalysator

Country Status (11)

Country Link
US (1) US5356851A (de)
EP (1) EP0564329B1 (de)
JP (1) JPH0623269A (de)
KR (1) KR100251260B1 (de)
CN (1) CN1046215C (de)
CA (1) CA2093272C (de)
DE (1) DE69315466T2 (de)
ES (1) ES2112403T3 (de)
FR (1) FR2689419B1 (de)
IN (1) IN181541B (de)
TW (1) TW327136B (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0685552A1 (de) * 1994-06-01 1995-12-06 Institut Francais Du Petrole Verfahren und Anlage für die selektive Hydrierung von katalytischen Crackbenzinen
US7919431B2 (en) 2003-09-03 2011-04-05 Synfuels International, Inc. Catalyst formulation for hydrogenation
US8013197B2 (en) 2005-02-18 2011-09-06 Synfuels International, Inc. Absorption and conversion of acetylenic compounds

Families Citing this family (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5696293A (en) * 1993-03-01 1997-12-09 Nippon Paint Co., Ltd. Catalyst composition for producing polyether polyamine and production method of polyether polyamine by use of the catalysts composition
FR2713957B1 (fr) * 1993-12-16 1996-02-02 Inst Francais Du Petrole Catalyseurs de déshydrogénation de paraffines C3-C20 et sa préparation.
US5422331A (en) * 1994-02-25 1995-06-06 Engelhard Corporation Layered catalyst composition
CN1053460C (zh) * 1996-04-16 2000-06-14 中国石油化工集团公司 用于重、渣油催化加氢的分散型催化剂
US6127310A (en) * 1997-02-27 2000-10-03 Phillips Petroleum Company Palladium containing hydrogenation catalysts
US6107237A (en) * 1997-07-10 2000-08-22 University Of Florida Homogeneous metathesis/heterogeneous hydrogenation
DE19839459A1 (de) 1998-08-29 2000-03-02 Basf Ag Katalysator und Verfahren zur Selektivhydrierung ungesättigter Verbindungen in Kohlenwasserstoffströmen
DE19840373A1 (de) 1998-09-04 2000-03-09 Basf Ag Katalysator und Verfahren zur Selektivhydrierung ungesättigter Verbindungen in Kohlenwasserstoffströmen
DE10020049A1 (de) * 1999-04-26 2001-01-11 Inst Francais Du Petrole Herstellung eines Katalysators, der ein Metall aus der Gruppe VIII und ein zusätzliches Metall enthält, das als wasserlösliche organmetallische Verbindung eingeleitet wird, sowie seine Verwendung für die Kohlenwasserstoffumwandlung
US6967063B2 (en) 2001-05-18 2005-11-22 The University Of Chicago Autothermal hydrodesulfurizing reforming method and catalyst
GB0119327D0 (en) * 2001-08-08 2001-10-03 Johnson Matthey Plc Catalyst
JP4020410B2 (ja) * 2001-12-28 2007-12-12 大研化学工業株式会社 炭素物質製造用触媒
US7378369B2 (en) * 2002-07-26 2008-05-27 Sud-Chemie Inc. Nickel supported on titanium stabilized promoted calcium aluminate carrier
US20040077496A1 (en) * 2002-07-26 2004-04-22 Shizhong Zhao Catalyst
US7208136B2 (en) * 2003-05-16 2007-04-24 Battelle Memorial Institute Alcohol steam reforming catalysts and methods of alcohol steam reforming
WO2004110966A1 (en) * 2003-05-29 2004-12-23 Dow Global Technologies, Inc. Dehydrogenattion of alkyl aromatic compound over a gallium-zinc catalyst
US7045670B2 (en) * 2003-09-03 2006-05-16 Synfuels International, Inc. Process for liquid phase hydrogenation
US7183451B2 (en) * 2003-09-23 2007-02-27 Synfuels International, Inc. Process for the conversion of natural gas to hydrocarbon liquids
US7208647B2 (en) * 2003-09-23 2007-04-24 Synfuels International, Inc. Process for the conversion of natural gas to reactive gaseous products comprising ethylene
US20050096217A1 (en) * 2003-10-29 2005-05-05 Sud-Chemie, Inc. Selective hydrogenation catalyst
US20050113614A1 (en) * 2003-11-24 2005-05-26 Lowe David M. Catalyst and process for selective hydrogenation
US7199273B2 (en) * 2003-11-24 2007-04-03 Exxonmobil Chemical Patents, Inc. Selective hydrogenation of alkynes and/or diolefins
US7220701B2 (en) * 2003-11-24 2007-05-22 Exxonmobil Chemical Patents Inc. Catalyst and process for selective hydrogenation
US7220700B2 (en) * 2003-11-24 2007-05-22 Exxonmobil Chemical Patents Inc. Catalyst and process for selective hydrogenation
FR2878530B1 (fr) * 2004-11-26 2008-05-02 Inst Francais Du Petrole Procede d'hydrotraitement d'une essence olefinique comprenant une etape d'hydrogenation selective
US20070123418A1 (en) * 2005-11-28 2007-05-31 Hyun-Sik Han Catalyst composition containing gallium for purifying exhaust gases of internal combustion engine
KR100808187B1 (ko) * 2006-03-21 2008-02-29 엘지전자 주식회사 스캐닝 디스플레이 장치
FR2909571B1 (fr) 2006-12-11 2009-10-02 Inst Francais Du Petrole Catalyseur prepare par impregnation d'une solution aqueuse contenant des particules oxy(hydroxy)de d'un cation en interaction avec une espece moleculaire d'un metal du groupe viii
EP2242735A2 (de) * 2008-01-07 2010-10-27 Danmarks Tekniske Universitet - DTU Katalysator, verfahren zur selektiven hydrierung von acetylen zu ethylen und verfahren zur herstellung des katalysators
EP2376224A1 (de) 2008-12-18 2011-10-19 Saudi Basic Industries Corporation Selektive katalytische hydrierung von alkinen in entsprechende alkene
FR2949078B1 (fr) 2009-08-17 2011-07-22 Inst Francais Du Petrole Procede de preparation d'un catalyseur supporte ni/sn pour l'hydrogenation selective d'hydrocarbures polyinsatures
FR2949077B1 (fr) 2009-08-17 2011-07-22 Inst Francais Du Petrole Procede de preparation d'un catalyseur supporte a base de ni et d'un metal du groupe ib pour l'hydrogenation selective d'hydrocarbures polyinsatures
US8648225B2 (en) 2010-04-12 2014-02-11 Chevron Phillips Chemical Company Lp Process for hydrogenating highly unsaturated hydrocarbons and catalyst therefor
CN110871076B (zh) * 2018-08-30 2022-09-20 中国石油化工股份有限公司 一种制备甲基异丁基醇的催化剂、制备方法及应用
CN113751021B (zh) * 2020-06-05 2023-09-05 台州学院 一种用于对硝基苯乙烯加氢制对氨基苯乙烯的催化剂及其制备方法和应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1004316B (de) * 1953-09-10 1957-03-14 Standard Oil Co Verfahren zur Herstellung eines Katalysators zur Hydrierung von Kohlenwasserstoffen
FR2091114A5 (de) * 1970-05-04 1972-01-14 Shell Int Research
FR2103122A5 (en) * 1970-07-24 1972-04-07 Phillips Petroleum Co Dehydrogenation/dehydrocyclisation catalyst - of nickel/platinum metal-carrier type modified with indium/gallium oxide
FR2594711A1 (fr) * 1986-02-26 1987-08-28 Inst Francais Du Petrole Procede de fabrication de catalyseurs contenant du platine, un halogene et au moins un metal additionnel, utilisables pour la conversion d'hydrocarbures par hydroreformage

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL102759C (de) * 1957-02-05 1900-01-01
US3892657A (en) * 1972-07-17 1975-07-01 Universal Oil Prod Co Hydrocarbon conversion with a multimetallic catalytic composite
GB1499297A (en) * 1976-06-29 1978-01-25 Kogan S Catalyst for dehydrogenation of paraffin hydrocarbons to olefines and method of preparing such a catalyst
US4337329A (en) * 1979-12-06 1982-06-29 Nippon Zeon Co., Ltd. Process for hydrogenation of conjugated diene polymers
US4486547A (en) * 1981-11-05 1984-12-04 Uop Inc. Indium-containing dehydrogenation catalyst
FR2556235A1 (fr) * 1983-12-09 1985-06-14 Pro Catalyse Procede de fabrication d'un catalyseur a base d'alumine
GB8529245D0 (en) * 1985-11-27 1986-01-02 British Petroleum Co Plc Chemical process
US4906800A (en) * 1986-11-17 1990-03-06 The Standard Oil Company Procedure for imparting selectivity to hydrogenation catalysts and method for using the same
AU628031B2 (en) * 1987-11-17 1992-09-10 Mobil Oil Corporation A dehydrogenation and dehydrocyclization catalyst, its synthesis and use
IT1243771B (it) * 1990-08-01 1994-06-28 Eniricerche Spa Catalizzatore di deidroisomerizzazione e suo uso nella preparazione di isobutene da n-butano
US5219816A (en) * 1991-12-20 1993-06-15 Exxon Research & Engineering Company Dehydrogenation catalysts and process for preparing the catalysts

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1004316B (de) * 1953-09-10 1957-03-14 Standard Oil Co Verfahren zur Herstellung eines Katalysators zur Hydrierung von Kohlenwasserstoffen
FR2091114A5 (de) * 1970-05-04 1972-01-14 Shell Int Research
FR2103122A5 (en) * 1970-07-24 1972-04-07 Phillips Petroleum Co Dehydrogenation/dehydrocyclisation catalyst - of nickel/platinum metal-carrier type modified with indium/gallium oxide
FR2594711A1 (fr) * 1986-02-26 1987-08-28 Inst Francais Du Petrole Procede de fabrication de catalyseurs contenant du platine, un halogene et au moins un metal additionnel, utilisables pour la conversion d'hydrocarbures par hydroreformage

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0685552A1 (de) * 1994-06-01 1995-12-06 Institut Francais Du Petrole Verfahren und Anlage für die selektive Hydrierung von katalytischen Crackbenzinen
FR2720754A1 (fr) * 1994-06-01 1995-12-08 Inst Francais Du Petrole Procédé et installation pour le traitement par hydrogénation sélective d'une essence de craquage catalytique.
US7919431B2 (en) 2003-09-03 2011-04-05 Synfuels International, Inc. Catalyst formulation for hydrogenation
EP2444154A1 (de) 2003-09-03 2012-04-25 Synfuels International, Inc. Verfahren zum Screening einer Katalysatorformulierung zur selektiven Flüssigphasen-Hydrierung
EP2444155A1 (de) 2003-09-03 2012-04-25 Synfuels International, Inc. Verfahren zur Herstellung einer Katalysatorformulierung zur Hydrierung
US8247340B2 (en) 2003-09-03 2012-08-21 Synfuels International, Inc. Catalyst formulation for hydrogenation
US8013197B2 (en) 2005-02-18 2011-09-06 Synfuels International, Inc. Absorption and conversion of acetylenic compounds

Also Published As

Publication number Publication date
FR2689419A1 (fr) 1993-10-08
CN1082458A (zh) 1994-02-23
KR930021262A (ko) 1993-11-22
CA2093272A1 (fr) 1993-10-03
DE69315466T2 (de) 1998-03-26
CN1046215C (zh) 1999-11-10
TW327136B (en) 1998-02-21
FR2689419B1 (fr) 1994-09-30
US5356851A (en) 1994-10-18
IN181541B (de) 1998-07-11
ES2112403T3 (es) 1998-04-01
EP0564329B1 (de) 1997-12-03
KR100251260B1 (ko) 2000-04-15
CA2093272C (fr) 2004-06-22
JPH0623269A (ja) 1994-02-01
DE69315466D1 (de) 1998-01-15

Similar Documents

Publication Publication Date Title
EP0564329B1 (de) Gruppe-VIII Metal und Gruppe-IIIA Metal an einem Träger enthaltender Katalysator
EP0564328B1 (de) Verfahren zur selektiven Hydrierung von Kohlenwasserstoffen
CA1045168A (fr) Procede d'hydrodealkylation d'hydrocarbures alkyl aromatiques
CA2270574A1 (fr) Catalyseurs d'hydrogenation selective contenant du palladium et au moins un element choisi parmi l'etain et le plomb
FR2674769A1 (fr) Catalyseur du type galloaluminosilicate contenant du gallium, un metal noble de la famille du platine et au moins un metal additionnel, et son utilisation en aromatisation des hydrocarbures.
EP2287275B1 (de) Verfahren zur Herstellung eines geträgerten Katalysators auf Basis von Ni und eines Metalls der Gruppe IB zur selektiven Hydrierung polyungesättigter Kohlenwasserstoffe
FR2611739A1 (fr) Procede d'activation d'un catalyseur d'isomerisation de paraffines normales
FR2742679A1 (fr) Catalyseur d'hydrogenation selective et procede utilisant ce catalyseur
EP0422968B1 (de) Hydrogenation von Citral
EP0256945B1 (de) Auf Mordenit basierter Katalysator für die Isomerisierung von geradkettigen Paraffinen
EP0623664B1 (de) Katalytisches Hydroreformierungsverfahren
EP0623387B1 (de) Katalytisches Hydrierverfahren
FR2704773A1 (fr) Procédé de préparation de catalyseurs utilisables en déshydrogénation.
CA2123072C (fr) Procede de preparation de catalyseur applicable a la deshydrogenation
EP0955090B1 (de) Katalysator zur Hydrierung von aromatischen Kohlenwasserstoffen in schwefelhaltigen Kohlenwasserstoffeinsätzen
FR2502142A1 (de)
BE1002425A4 (fr) Procede de preparation de catalyseurs contenant un metal du groupe du platine.
JP2004504135A (ja) イリジウム開環触媒上でのナフテンの開環
EP0599728A1 (de) Verfahren zur selektiven Hydrierung von Verbindungen mit endo- und exocyklischen ungesältigten Bindungen
EP0507658A1 (de) Verfahren zur Reduktion in einem organischen Medium eines Raffinierungskatalysators vor seiner Anwendung
FR2720957A1 (fr) Catalyseur d'hydrogénation contenant du palladium et au moins un métal alcalin ou alcalino terreux et procédé d'hydrogénation utilisant ce catalyseur.
FR2735388A1 (fr) Catalyseurs contenant du silicium et du titane, zirconium, hafnium, cobalt, nickel et/ou zinc, utilisables dans les reactions de transformation d'hydrocarbures
FR2735390A1 (fr) Catalyseurs a faibles teneurs en lanthanide et contenant du silicium, utilisables dans les reactions de transformation des hydrocarbures

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): BE DE ES GB IT NL PT

17P Request for examination filed

Effective date: 19940310

17Q First examination report despatched

Effective date: 19951030

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

ITF It: translation for a ep patent filed

Owner name: DE DOMINICIS & MAYER S.R.L.

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE ES GB IT NL PT

REF Corresponds to:

Ref document number: 69315466

Country of ref document: DE

Date of ref document: 19980115

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19980112

REG Reference to a national code

Ref country code: PT

Ref legal event code: SC4A

Free format text: AVAILABILITY OF NATIONAL TRANSLATION

Effective date: 19971212

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2112403

Country of ref document: ES

Kind code of ref document: T3

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

REG Reference to a national code

Ref country code: DE

Ref legal event code: R081

Ref document number: 69315466

Country of ref document: DE

Owner name: IFP ENERGIES NOUVELLES, FR

Free format text: FORMER OWNER: INSTITUT FRANCAIS DU PETROLE, RUEIL-MALMAISON, HAUTS-DE-SEINE, FR

Effective date: 20110331

Ref country code: DE

Ref legal event code: R081

Ref document number: 69315466

Country of ref document: DE

Owner name: IFP ENERGIES NOUVELLES, FR

Free format text: FORMER OWNER: INSTITUT FRANCAIS DU PETROLE, RUEIL-MALMAISON, FR

Effective date: 20110331

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: PT

Payment date: 20120201

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20120322

Year of fee payment: 20

Ref country code: GB

Payment date: 20120327

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20120402

Year of fee payment: 20

Ref country code: DE

Payment date: 20120411

Year of fee payment: 20

Ref country code: NL

Payment date: 20120403

Year of fee payment: 20

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69315466

Country of ref document: DE

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69315466

Country of ref document: DE

BE20 Be: patent expired

Owner name: INSTITUT FRANCAIS DU *PETROLE

Effective date: 20130324

REG Reference to a national code

Ref country code: NL

Ref legal event code: V4

Effective date: 20130324

Ref country code: PT

Ref legal event code: MM4A

Free format text: MAXIMUM VALIDITY LIMIT REACHED

Effective date: 20130324

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20130323

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20130323

Ref country code: DE

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20130326

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20120321

Year of fee payment: 20

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20130722

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: PT

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20130403